One step process for preparing A 1,3-DIOL

ABSTRACT

The invention provides a process for an improved oxirane hydroformylation catalyst, the improved oxirane hydroformylation catalyst, and a one step process for preparing a 1,3-diol in the presence of such a catalyst. One process for preparing the hydroformylation catalyst involves:  
     a) forming a complex (A) by contacting a ruthenium(0) compound with a ditertiary phosphine ligand; and  
     b) forming a complex (B) by subjecting complex (A) to a redox reaction with a cobalt(0) carbonyl compound. This catalyst is used in a one step hydroformylation process for preparing a 1,3-diol, comprising the reaction of an oxirane with syngas at hydroformylation conditions in an inert solvent in the presence of the above hydroformylation catalyst where recovery of product is preferably accomplished via phase separation of a diol rich phase from the bulk reaction liquor.

FIELD OF THE INVENTION

[0001] The present invention relates to a one step process for preparinga 1,3-diol, and 1,3-propanediol in particular.

BACKGROUND OF THE INVENTION

[0002] 1,3-Diols have plenty of uses, particularly in the synthesis ofpolymers. For instance, “CORTERRA” (trademark) is a polyester made of1,3-propanediol (hereinafter ‘PDO’) and terephthalic acid, which polymerhas outstanding properties. Other 1,3-diols may find similar use.Commercially attractive routes to prepare such 1,3-diols are thereforehighly desirable.

[0003] U.S. Pat. No. 5,304,691 and the art described therein relates toa process for making PDO and HPA (3-hydroxypropanal, a3-hydroxyaldehyde). In this particular patent, PDO and HPA are made byintimately contacting an oxirane (ethylene oxide, hereinafter ‘EO’), aditertiary phosphine-modified cobalt carbonyl catalyst, a rutheniumcatalyst promoter, and syngas (carbon monoxide and hydrogen) in an inertreaction solvent at hydroformylation reaction conditions. A PDO yield ofup to 86-87 mole % is reported, using a catalyst comprising cobaltligated with 1,2-bis(9-phosphabicyclononyl)ethane as bidentate ligand,and either triruthenium(0) dodecarbonyl or bis[ruthenium tricarbonyldichloride] as cocatalyst.

[0004] As mentioned, this process typically results in the synthesis ofa mixture of HPA and PDO. However, it would be much more attractive toproduce PDO in a single step, or in a higher yield, obviously withoutco-producing impurities that inhibit the use of PDO in the preparationof polymers etc. In order for this process to be particularlysuccessful, recycle of the catalyst without significant deterioration ofperformance is needed. Surprisingly such a process, and a catalystsuitably used therein has now been found.

SUMMARY OF THE INVENTION

[0005] Accordingly the invention provides a process for an improvedoxirane hydroformylation catalyst, the improved oxirane hydroformylationcatalyst, and a one step process for preparing a 1,3-diol in thepresence of such a catalyst where recovery of product is preferablyaccomplished via phase separation of a diol rich phase from the bulkreaction liquor.

[0006] The process for preparing an improved oxirane hydroformylationcatalyst involves:

[0007] a) forming a complex (A) by contacting a ruthenium(0) compoundwith a ditertiary phosphine ligand; and

[0008] b) forming a complex (B) by subjecting complex (A) to a redoxreaction with a cobalt(0) carbonyl compound.

[0009] The novel oxirane hydroformylation catalyst involves complex (B),which is postulated to be a ruthenium(+1)-phosphine bidentate:cobalt(−1) complex. The characterizing feature of the novel catalyst is thatthe metal being ligated is ruthenium, rather than cobalt as in the '691U.S. patent referred to above. Indeed, upon analysis of both systems adistinct difference in the catalysts was noted in the IR spectra. The IRspectrum of the catalyst according to the present invention revealed thepresence of phosphorus-ruthenium bands at 2107, 2053, and 2040 cm⁻¹,which are not present in the IR spectrum of the catalyst according tothe invention of the '691 patent.

[0010] Finally, the invention also provides a one step process forpreparing a 1,3-diol, comprising the reaction of an oxirane with syngasat hydroformylation conditions in an inert solvent in the presencecomplex (B) as catalyst.

BRIEF DESCRIPTION OF THE FIGURES

[0011]FIG. 1 is a comparison of the in-situ IR spectrum of the inventioncatalyst (as prepared) with the in-situ IR spectrum of a comparisoncatalyst (as prepared).

[0012]FIG. 2 is a comparison of the in-situ IR spectrum of the HPAabsorbance at 1728 cm⁻¹ over the course of the reaction using a catalystin accordance with the present invention, as compared to the comparisoncatalyst.

[0013]FIG. 3 is an IR spectrum of catalyst regions of the isolated solidof example 5.

DETAILED DESCRIPTION OF THE INVENTION

[0014] Oxiranes of up to 10 carbon atoms, preferably up to 6 carbonatoms, and ethylene oxide in particular may be converted into theircorresponding 1,3-diols by the hydroformylation reaction with syngas inthe presence of complex (B) as catalyst.

[0015] The 1,3-diols are made by charging the oxirane, catalyst,optional cocatalyst and/or catalyst promoter and reaction solvent to apressure reactor with the introduction of syngas (a mixture of hydrogenand carbon monoxide, suitably in a molar ratio of 1:1 to 8:1, preferably2:1 to 6:1) under hydroformylation conditions.

[0016] The process of the present invention comprises batch-typeprocesses, continuous processes and mixed forms thereof.

[0017] For best results, the process is conducted under conditions ofelevated temperature and pressure. Reaction temperatures range fromambient temperature to 150° C., preferably from 50 to 125° C., and mostpreferably from 60 to 110° C. The reaction pressure (total pressure, orpartial pressure if inert gaseous diluents are used) is desirably in therange from 5 to 15 MPa, preferably from 8 to 10 MPa. In a batch process,the reaction will generally be complete within 1.5 to 5 hours. Thereaction solvent is preferably inert, meaning that it is not consumedduring the course of the reaction. Ideal solvents for the inventionprocess will solubilize the feed and products during the course of thereaction, but allow phase separation at reduced temperatures. Suitablesolvents are described in U.S. Pat. No. 5,304,691 incorporated herewithby reference. For instance, good results may be achieved with ethers,including cyclic and acyclic ethers, optionally in combination with analcohol or aromatic hydrocarbon. Excellent results have been achievedwith methyl tert butyl ether (MTBE) and a mixture of toluene withchlorobenzene.

[0018] The process of the present invention, in respect of the preferredembodiment on the synthesis of PDO, can be conveniently described asfollows. Separate, combined or staged streams of EO, syngas and catalystare charged to a reaction vessel, which can be a pressure reactionvessel such as a bubble column or a stirred autoclave, operatedbatch-wise or in a continuous manner.

[0019] The components of the feed streams are contacted in a suitablereaction solvent in the presence of the catalyst of the presentinvention. The EO will preferably be maintained throughout the reactionin a concentration not less than about 0.2% by weight, generally withinthe range of 0.2 to 20% by weight, preferably 1 to 10% by weight, basedon the total weight of the reaction mixture. The process of theinvention can be carried out in a continuous mode, whilst maintainingsaid EO concentration, by for instance staged EO addition.

[0020] At the conclusion of the hydroformylation reaction, the productmixture is recovered by conventional methods such as selectiveextraction, fractional distillation, phase separation, selectivecrystallization and the like. The unreacted starting materials as wellas the catalyst and reaction solvent may, and preferably are recycledfor further use.

[0021] In a preferred manner of running the process, reaction conditionssuch as oxirane concentration, catalyst concentration, solvent, productconcentration, reaction temperature and the like are selected such as toachieve a homogeneous reaction mixture at elevated temperatures andcause a partitioning of the reaction mixture into an upper solvent phasecontaining much of the catalyst and a lower phase containing most of the1,3-propanediol upon cooling the mixture. Such a partitioningfacilitates isolation and recovery of product, recyle of catalyst andremoval of heavy ends from the solvent system. This process is referredto as a phase separation catalyst recycle/product recovery method.

[0022] In this process, the reactor contents are allowed to settle orare transferred to a suitable vessel at or near reaction pressure whereupon slight or considerable cooling distinct phases may form that aresubstantially different, being considerably rich in product or incatalyst and solvent. The phase rich in catalyst and solvent is directlyrecycled for further reaction with feed materials. Product is recoveredfrom the product rich phase by conventional methods.

[0023] It is essential that the reaction is run such that product diolmaintains concentration levels in the reaction mix suitable for phaseseparation. For example, concentration of 1,3-propanediol can be betweenless than 1 and greater than 50% by weight, generally between 8 and 32%by weight and preferably between 16 and 20% w. Temperature duringquiescent settling of phases can be between just above the freezingpoint of the reaction mixture up to at least 150° C. and very likelyhigher, generally between 27 and 97° C., and preferably between 37 and47° C. The EO concentration is maintained to avoid the formation oflight alcohols and aldehydes that are miscibilizing agents. Oxiraneswill preferably be maintained throughout the reaction in a concentrationnot less than about 0.2% by weight, generally within the range of 0.2 to20% by weight, preferably 1 to 10% by weight, based on the total weightof the reaction. The reaction can be run with a two-phase system.However, yields and selectivities are maximized when high concentrationsof product are present in a single phase reaction and subsequent phaseseparation occurs upon cooling.

[0024] Partitioning of the reaction mixture can be promoted by theaddition of a phase-split inducing agent. Suitable agents includeglycols such as ethylene glycol and linear alkanes such as dodecane.Such an agent will be added to the reaction mixture in an amount withinthe range of about 2 to 10% w, preferably 4 to 6% w based on the totalreaction mixture. Alternate methods include addition of 1,3-propanediolinto the reaction mixture to bring product concentration up to thetarget proportion. Also, miscibilizing alcohols and agents with similarpolarity such as ethanol, propanol and isopropanol can be addedinitially, then removed prior to, and subsequently inducing the phaseseparation.

[0025] It is essential in the above described process that as catalyst acomplex (B) is used. Complex (B) is believed to comprise a novel classof ruthenium-modified catalysts. The characterizing feature of thisnovel class involves an oxidized ruthenium metal that is ligated by atertiary diphosphine ligand, with a cobalt compound as counter ion, thatmay be but preferably is not ligated by a phosphorus ligand.

[0026] One compound of this complex comprises the phosphorus ligand. Asmentioned, this ligand is a tertiary diphosphine of the general formula:

RRP—Q—PR′R′

[0027] wherein each group R and R′independently or jointly is ahydrocarbon moiety of up to 30 carbon atoms, and Q is an organicbridging group of 2 to 4 atoms in length. The group R or R′, whenmonovalent, may be alkyl, cycloalkyl, bicycloalkyl or aryl, andpreferably of up to 20 carbon atoms, more preferably of up to 12 carbonatoms. Alkyl and/or cycloalkyl groups are preferred. The group Q ispreferably composed of carbon atoms, which may form part of a ringsystemsuch as a benzene ring or a cyclohexane ring. More preferably Q is analkylene group of 2, 3 or 4 carbon atoms in length, most preferably of 2carbon atoms in length. A non-limiting list of illustrative diphosphinesof this class include 1,2-bis(dimethylphosphino)ethane;1,2-bis(diethylphosphino)ethane; 1,2-bis(diisobutylphosphino)ethane;1,2-bis(dicyclohexylphosphino)ethane;1,2-bis(2,4,4-trimethylpentylphosphino)ethane;1,2-bis(diethylphosphino)propane; 1,3-bis(diethylphosphino)propane;1-(diethylphosphino)-3-(dibutylphosphino)propane,1,2-bis(diphenylphosphino)ethane; 1,2-bis(dicyclohexylphosphino)ethane;1,2-bis(2-pyridyl, phenylphosphanyl)benzene;1,2-bis(dicyclopentyphosphino)ethane;1,3-bis(2,4,4-trimethylpentyphosphino)propane;1,2-bis(diphenyl-phosphino) benzene, and the like. These groups R and R′may be substituted with non-hydrocarbon groups themselves. Both groups Rand/or both groups R′ may also form a ring with the phosphorus atom(s),such as a phosphacycloalkane of from 5 to 8 atoms. Examples on 5-ringsystems (phospholano-based ligands) include 1,2-bis(phospholano)ethane,1,2-bis(2,5-dimethylphospholano)benzene, optically pure (R,R), (R,S),(S,S) 1,2-bis(2,5-dimethylphospholano)ethane or its racemic mixture, andthe like. The ring itself may be part of a multiring system. Examples ofsuch ring systems may be found in the aforementioned '691 patent and inWO-A-9842717 (herewith incorporated by reference). In the formerphosphabicyclononyl groups are described, in the latter adamantyl-likegroups and phosphatrioxatricyclodecyl groups in particular aredescribed. Diphosphines wherein both groups R and R′ form a ring withthe phosphorus atom are preferred. The most preferred ligands are1,2-P,P′-bis(9-phosphabicyclo[3.3.1] and/or [4.2.1]nonyl) ethane(hereinafter B9PBN-2), its 1,2-P,P′-propane and/or its 1,3-P,P′-propaneanalogue (hereinafter B9PBN-3).

[0028] Ditertiary phosphine ligands are commercially available.Catalysts prepared therefrom are known in the art and their method ofpreparation are described in detail in U.S. Pat. Nos. 3,401,204 and3,527,818, which are both incorporated by reference herein. Thephosphine ligands may also be partially oxidized to phosphine oxides inthe manner described in the '691 patent.

[0029] The ratio of ligand to ruthenium atom may vary from 2:1 to 1:2,preferably from 3:2 to 2:3, more preferably from 5:4 to 4:5 and is mostpreferably about 1:1. It is hypothesized that this results in a tertiarydiphospine ruthenium tricarbonyl compound, but it might also be abis(tertiary diphosphine ruthenium) pentacarbonyl compound. Unligatedruthenium carbonyl is believed to be an inactive species, and thecatalyst preparation therefore seeks to ligate each ruthenium atom.

[0030] The counter ion, for best results, is believed to be cobalttetracarbonyl ([Co(CO)₄]⁻), although the ion in the active catalyst maybe a modification thereof. Part of the cobalt compound may be modifiedwith (excess) tertiary diphosphine, e.g., up to 75 mole %, say up to 50mole % or less. However, the counter ion is preferably the non-ligatedcobalt tetracarbonyl mentioned before. Cobalt carbonyls can be generatedby reaction of a starting cobalt source such as cobalt hydroxide withsyngas, as described in J. Falbe, “Carbon Monoxide in OrganicSynthesis”, Springer-Verlag, NY (1970), or otherwise.

[0031] The oxidation state of the ruthenium atom is not entirely certain(in theory, ruthenium may have a valence of 0 to 8), which may evenchange during the course of the hydroformylation reaction. Accordingly,the molar ratio of ruthenium to cobalt may vary within relatively broadranges. Sufficient cobalt (0) should be added to completely oxidize allof the complexed ruthenium employed. An excess of coblat can be added,but is not of particular value. Suitably, the molar ratio varies from4:1 to 1:4, preferably from 2:1 to 1:3, more preferably from 1:1 to 1:2.

[0032] The catalyst, complex (B), may be made as follows hereafter. Thefirst step in the catalyst preparation is the synthesis of complex (A).This may be done by bringing a suitable Ru(0) source, e.g., trirutheniumdodecacarbonyl, in contact with the tertiary diphosphine. Alternatively,the triruthenium dodecacarbonyl may be replaced with less expensiveruthenium sources that in-situ form Ru(0), such as ruthenium(IV) oxide,hydrate.

[0033] The conditions at which these compounds are allowed to form acomplex are not critical. Temperature and pressure may vary within theranges already mentioned in respect of the hydroformylation reaction.Syngas may be used as gas cap during the complex formation. On the otherhand, it is preferable to use a solvent, preferably the solvent (if any)used in the hydroformylation reaction. Obviously, this solvent should becapable to dissolve the active catalyst, without affecting itsproperties. Suitable solvents include the ethers described before, andmethyl tertiary-butyl ether (MTBE) in particular.

[0034] The complex (A) may for instance be made by reacting trirutheniumdodecacarbonyl with a stoichiometric amount of a selected ligand in asolvent at a temperature within the range of 90 to 130° C., suitably 100to 110° C. under a carbon monoxide atmosphere, for a 1 to 3 hours (i.e.,until completion).

[0035] Next, the complex (A) is brought in contact with a suitablecobalt compound, again at the aforementioned (non critical) conditions.A suitable cobalt source is dicobalt octacarbonyl, but other cobalt(0)complexes, preferably with the exception of phosphine-modifiedcomplexes, may be used as well. For instance, the selected cobaltcarbonyl, and optional promoters, if any, are added to the solutionwhich is then maintained at the elevated temperature for a time of about15 to 60 minutes. This process is referred to as a step-wise preparationmethod.

[0036] Suitable cobalt sources also include salts which are reduced tothe zero valence state by heat-treatment e.g. in an atmosphere ofhydrogen and carbon monoxide. Examples of such salts comprise, forinstance, cobalt carboxylates such as acetates, octanoates, etc., whichare preferred, as well as cobalt salts of mineral acids such aschlorides, fluorides, sulfates, sulfonates, etc. Operable also aremixtures of these cobalt salts. It is preferred, however, that whenmixtures are used, at least one component of the mixture be cobaltalkanoate of 6 to 12 carbon atoms. The reduction may be performed priorto the use of the catalysts or it may be accomplished simultaneouslywith the hydroformylation process in the hydroformylation zone.

[0037] It is also within the scope of the present invention to preparecomplex (A) by a self-assembly method, wherein all catalyst componentsare brought together at the same time, but the conditions and inparticular the solvent, are selected such as to favor the formation of aligated ruthenium species, rather than a ligated cobalt species. Thepresence of the Ru-ligated species rather than the Co-phosphine speciesmay be confirmed by e.g. IR analysis.

[0038] In this respect it is emphasized that in the aforementioned U.S.Pat. No. 5,304,691 it was said that the form of the ruthenium is notcritical. Although it is suggested to use ruthenium complexes ofphosphines described in this reference, any such use is clearly toprepare tertiary phosphine-complexed cobalt carbonyl catalysts, withconsequently the loss of the phosphine-complexed ruthenium startingmaterial.

[0039] The optimum ratio of oxirane feed to complex (B) will in partdepend upon the particular complex employed. However, molar ratios ofoxirane to the cobalt within complex (B) from 2:1 to 10,000:1 aregenerally satisfactory, with molar ratios of from 50:1 to 500:1 beingpreferred.

[0040] Promoters, such as described in the aforementioned '691 patentmay be used. The currently preferred promoter, because of itsavailability and demonstrated promotion of EO conversion aredimethyldodecylamine and triethylamine.

[0041] Commercial operation will require efficient catalyst recoverywith multiple cycles of essentially complete recycle of catalyst to thereaction. The preferred catalyst recovery process involves separation ofthe two liquid phase mixture noted previously and recycle of the bulksolvent phase to the reactor and return therewith of at least 60 to 90%by weight of the starting catalyst.

[0042] The invention is further illustrated by the following examples.TABLE 1 Materials and formulations Co source CoOc Cobalt octoate DCODicobalt octacarbonyl Ru source TRC Triruthenium dodecacarbonyl BRCCBis(ruthenium tricarbonylchloride) Ligand B9PBN-21,2-P,P′-bis(9-phosphabicyclononyl)ethane BDEPE1,2-bis(diethylphosphino)ethane BDIPE 1,2-bis(diiosbutylphosphino)ethaneBDOPE 1,2-bis(2,4,4-trimethylpentylphosphino)ethane BDMPE(R,R)1,2-bis(dimethylphospholano)ethane Solvent MTBE Methyl-t-butylether T/CB 5:1 v/v mixture of toluene/chlorobenzene Oxirane EO Ethyleneoxide Promoter DMDA Dimethyldodecylamine NaAc Sodium acetate

[0043] The IR analysis was conducted with in situ cylindrical internalreflectance reactors of the type described by W. R. Moser, J. E.Cnossen, A. W. Wang, and S. A. Krouse in Journal of Catalysis, 1985, 95,21; sold by Spectra-Tech Inc. mated to a Nicolet Magna 550 spectrometer.The spectral region of interest includes both the catalyst bands andaldehyde intermediates in the region of 1500 to 2500 cm⁻¹.

EXAMPLE 1 Preparation of Complex (B)

[0044] In a dry box the following materials were loaded into a 50 mlstainless steel reactor fitted with optics for in-situ reactionmonitoring by mid IR analysis: 61 mg TRC (0.286 mmoles Ru), 171 mgB9PBN-2 (0.551 mmoles) and 17 ml of MTBE.

[0045] The reactor was sealed, removed from the dry box, placed into theoptical bench of an IR spectrometer, and pressurized to 2.2 MPa withcarbon monoxide. The reactor was heated to 105° C. and the progress ofthe complex (A) formation was monitored by IR. Once the temperaturereached 105° C., hydrogen was added to bring the gas composition to anapproximate 3:1 syngas ratio.

[0046] To this mixture was added a solution of 113 mg DCO and 47 mg ofDMDA dissolved in 5 ml of MTBE, using excess 1:1 syngas pressure tobring the total reactor pressure to 8.6 MPa. After an additional 35minutes at 105° C. the reactor was cooled.

Comparative Example A Preparation of a Ligated Co Catalyst as in U.S.Pat. No. 5,304,691

[0047] In a dry box the following materials were loaded into a 50 mlstainless steal reactor fitted with optics for in-situ reactionmonitoring by mid IR analysis: 228 mg CoOc (0.66 mmoles Co), 74 mg BRCC(0.289 mmoles Ru), 222 mg B9PBN-2 (0.715 mmoles), 18 mg sodium acetate(0.22 mmoles) and 23 ml T/CB.

[0048] The reactor was sealed, removed from the dry box, placed into theoptical bench of an IR spectrometer, and pressurized to 9.0 MPa with 4:1syngas. The reactor was heated to 130° C. and the progress of thecatalyst formation was monitored by IR.

EXAMPLE 2 Preparation of Complex (B) by Self-Assembly

[0049] To a 100 ml autoclave was charged in a manner similar toComparative Example A: 228 mg CoOc (0.66 mmole); 23 ml MTBE; 62 mg TRC(0.29 mmole); 167 mg B9PBN-2 (0.50 mmole); and 17 mg NaAc (0.21 mmole).Again the progress of the catalyst formation was monitored by IR.

[0050] Catalyst Analysis by IR

[0051] Upon addition of B9PBN-2 to TRC, the TRC bands at 2059, 2029 and2009 cm⁻¹ disappeared and an increase was noticed in bands at 1954, 1884and 1853 cm⁻¹. Upon addition of cobalt carbonyl the oxidation ofchelated ruthenium took place accompanied by an instantaneous shift inthe IR bands, generating characteristic bands at 2040, 2053, and 2107cm⁻¹ as well as a band at 1890 cm⁻¹ that is characteristic for the(unligated) cobalt carbonyl anion.

[0052] Referring to FIG. 1, the solid line is an in-situ IR spectrum ofthe complex (B) prepared as described in Example 1. The predominantcatalysts bands (at 2040, 2053, and 2107 cm⁻¹) are characteristic ofphosphine-modified ruthenium compounds. The dotted line is an in-situ IRspectrum of the comparative catalyst. The in-situ IR spectrum of thecomplex (B) prepared by the self-assembly method closely corresponded tothat of the catalyst made in Example 1.

EXAMPLE 3 Preparation of PDO

[0053] At 80° C. 1.1 g EO was added to the reaction mixture of Example1, using excess 1:1 syngas pressure. Syngas (1:1) was added as needed tothe reaction mixture to maintain the reaction pressure between 10.4 and11.1 MPa. The EO was allowed to react completely. When cooled, thereactor was opened and a two-phase liquid was isolated. GC analysisrevealed the primary EO-derived product in both phases was PDO. (Yieldof greater than 50 mole %) In a similar manner, the catalyst ofcomparative example A was used. However, the two-phase liquid isolatedat the end of this experiment was found to comprise a lower phaseshowing an approximately 50/50 mixture of PDO and HPA and an upper phasecontaining PDO, HPA and other materials. (Yield of greater then 50 mole%)

[0054] The progress of both reactions were tracked by IR, observing theintensity of absorbance of the intermediate 3-hydroxypropionaldehydecarbonyl band (1728 cm⁻¹). The results are reproduced FIG. 2.

[0055] Using the catalyst of the present invention, the aldehyde bandwas seen to rise only slightly at the onset of reaction and thendecrease rapidly as the HPA was converted into PDO. Said band increasedsteadily over the course of the reaction when the catalyst ofcomparative example A was used. Indicating the superior hydrogenatingability of the catalyst of the present invention.

Comparative Example B

[0056] The experiment of Example 3, using the catalyst of Comparativeexample A was essentially followed, with staged addition of EO (4steps). In about 4 to 6 hours 1,3-PDO was prepared in a yield of 66 mole% at 80% selectivity. Next, the crude liquid product was fractionallydistilled under vacuum (<0.1 kPa) to recover PDO as distillate productfraction. The remainder was recycled with additional EO and syngas, plusmake-up solvent for a second run. The PDO yield was found to be only 44mole %, with only 67% selectivity. When the remainder of this productwas recycled and allowed to catalyze a third run, the PDO yield hadessentially vanished (2 mole %).

EXAMPLE 4

[0057] The experiment of Example 3, using a catalyst corresponding tothat of Example 1, however using BDEPE instead was essentially followed,with staged addition of EO (4 steps). In about 4 to 6 hours PDO wasprepared in a yield of 48 mole % at 57% selectivity. Next, the crudeliquid product was fractionally distilled under vacuum (<0.1 kPa) torecover PDO as distillate product fraction. The remainder was recycledwith additional EO and syngas, plus make-up solvent for a second run.The PDO yield was found to be 40 mole %, with 54% selectivity. When thecatalyst was recycled and allowed to catalyze the reaction in thismanner for the tenth time, the PDO yield was still found to be 49 moles%, with 59% selectivity.

[0058] No apparent loss of catalyst activity was noticed over 12 EOadditions. Furthermore, P-NMR of the final product solution indicated nofree BDEPE, with most of the P-ligand still bound to the ruthenium. Itmay therefore be concluded that the novel catalysts of the presentinvention possess increased stability.

EXAMPLE 5

[0059] Various (scouting) experiments similar to that of Example 3 wereconducted, using a catalyst prepared by self assembly with an initialCo:Ru:ligand molar ratio of 2:1:2. The test results are described in thefollowing Table. TABLE 2 Ligand PDO Yield (mole %) PDO Selectivity (%)BDEPE 48-73 83-87 BDIPE 36-53 80-86 BDOPE 31 69 BDMPE 51-71 78-95

[0060] From these results it may be concluded that the catalysts of thepresent invention are invariably suitable for the one-step conversion ofoxiranes.

EXAMPLE 6 Preparation of Complex (B)

[0061] In a dry box the following materials were loaded into a 50 mlstainless steel reactor fitted with zinc sulfide optics for in-situreaction monitoring by mid IR analysis: 128 mg TRC (0.600 mmoles Ru),186 mg B9PBN-2 (0.600 mmoles), 9 ml of toluene and 9 ml of MTBE.

[0062] The reactor was sealed, removed from the dry box, placed into theoptical bench of an IR spectrometer, and pressurized to 1.7 MPa withcarbon monoxide. The reactor was heated to 105° C. and the progress ofthe complex (A) formation was monitored by IR. Upon heating the TRCbands at 2059, 2029 and 2009 cm−1 disappeared and an increase wasnoticed in bands at 1954, 1882 and 1861 cm−1. After one hour at 105° C.,hydrogen was added to bring the gas composition to an approximate 3:1syngas ratio, 8.29 MPa, and a solution of 105 mg DCO (0.614 mmoles Co)dissolved in 6 ml of MTBE was added via excess syn gas pressure,bringing the total reactor pressure to 10.3 MPa. Upon addition of cobaltcarbonyl, the oxidation of chelated ruthenium took place accompanied byan instantaneous shift in the IR bands, generating characteristic bandsat 2040, 2053, and 2107 cm−1 as well as a band at 1890 cm−1 that ischaracteristic for the (unligated) cobalt carbonyl anion. This was heldat 105° C. for 1.5 hours without apparent change in the catalystcomposition. Upon heating to 130° C., the mid IR spectrum indicated noalteration in the catalyst composition. The reactor was cooled to roomtemperature, opened and 0.25 grams of yellow-orange catalyst solids wereisolated by suction filtration and dried in vacuo. An infrared spectrumof the isolated solid is shown in FIG. 3, the only bands metal carbonylbands present are due to phosphine ligated ruthenium (I) with a cobalt(−I) tetracarbonyl anion. No other cobalt carbonyls are present. Thiscomplex is identical to catalyst solids isolated from a one step1,3-propanediol reaction of the present invention.

EXAMPLE 7 Use of Isolated Complex (B) for Preparation of 1,3-propanediolin a Single Step

[0063] In a dry box 0.24 grams of catalyst solids from Example 5 and 23ml of MTBE were loaded into a 50 ml stainless steal reactor fitted withzinc sulfide optics for in-situ reaction monitoring by mid IR analysis.The reactor was sealed, removed from the dry box, placed into theoptical bench of an IR spectrometer, and pressurized to 7.0 MPa with4:1; hydrogen:carbon monoxide. The reactor was heated to 90° C. and 1.9grams of EO was added to the reaction mixture using excess 1:1 synthesisgas pressure. The 1:1 synthesis gas was added to the reaction mixture tomaintain a reactor pressure between 10.1 and 10.8 MPa. Within an hourthe first aliquot of ethylene oxide was consumed and a second 1.9 grams(3.8 grams total) of ethylene oxide was injected into the reactor. Thereaction mixture again rapidly consumed synthesis gas, make up gas beingadded as needed. The reaction was run to essentially complete EOconsumption during the entire reaction, the IR spectrum of the catalystregion remains the same as the starting catalyst solids. Upon coolingand opening the reactor a two phase mixture was obtained. GC analysis ofboth phases revealed a PDO yield in excess of 50% with only traceamounts of HPA detected.

EXAMPLE 8 Phase Separation Catalyst Recycle/Product Recovery Processwith Catalyst Formed by Self Assembly

[0064] In an inert atmosphere drybox, to a 300 ml autoclave, 1.85 grams(5.35 mmole Co) cobalt(II) ethylhexanoate, 1.392 grams (4.48 mmole)1,2-bis(9-phosphacyclononyl) ethane, 0.509 grams (2.3 mmole Ru)triruthenium dodecylcarbonyl, 145.85 grams methyl-tert-butyl ether(MTBE) and 0.30 grams dimethyldodecyl amine was added. The autoclavebody was sealed and fitted to a benchscale process unit. Under aheadspace of 4:1 H₂:CO ratio syngas at 1500 psig the mixture was allowedto reach equilibrium and preform catalyst over 2 hours at 130° C.Reactor temperature was reduced to 90° C. An addition of 16.96 grams ofethylene oxide (EO) was made and allowed to react with syngas feed at a2:1 H₂:CO ratio until the EO is substantially but not completelyconsumed. The reactor content was transferred under reaction conditionsto a phase separation vessel where phase separation began immediately.From the vessel, 12.94 grams lower layer material was isolated. Theupper layer reaction liquor was recycled back to the reactor.Compositions of the upper and lower layer are given in Table 3. Catalystpartition data is shown in Table 4. The product, 1,3-propanediol, wasproduced at an average rate of 20 g/L/hr.

EXAMPLE 9 Phase Separation Process, Recycle 1

[0065] The recycled reaction liquor from example 8 was heated to 90° C.An addition of 14.74 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 H₂:CO ratio syngas at 1500 psig until the EOwas substantially consumed. The reactor contents were transferred undersyngas pressure to a phase separation vessel where phase separationbegan immediately resulting in the isolation of 8.22 grams of lowerlayer material. Upper layer reaction liquor was recycled back to thereactor. Compositions of the upper and lower layer are given in Table 3.Catalyst partition data is shown in Table 4. The averaged reaction ratethrough this recycle gave 14 g/L/hr.

EXAMPLE 10 Phase Separation Process, Recycle 2

[0066] The recycled reaction liquor from example 9 was heated to 90° C.An addition of 14.74 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 H₂:CO ratio syngas at 1500 psig. The reactorcontents were transferred under syngas pressure to a phase separationvessel where phase separation began immediately and 8.50 grams of lowerlayer material was isolated. Upper layer reaction liquor was recycledback to the reactor. Compositions of the upper and lower layer are givenin Table 3. Catalyst partition data is shown in Table 4. The averagedreaction rate through this recycle gave 37 g/L/hr.

EXAMPLE 11 Phase Separation Process, Recycle 3

[0067] The recycled reaction liquor from example 10 was heated to 90° C.An addition of 14.74 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 H₂:CO ratio syngas at 1500 psig. The reactorcontents were,transferred under syngas pressure to a phase separationvessel where phase separation began immediately and 19.50 grams of lowerlayer material was isolated. Upper layer reaction liquor was recycledback to the reactor. Compositions of the upper and lower layer are givenin Table 3. Catalyst partition data is shown in Table 4. The averagedreaction rate through this recycle gave 49 g/L/hr.

EXAMPLE 12 Phase Separation Process, Recycle 4

[0068] The recycled reaction liquor from example 11 was heated to 90° C.An addition of 14.74 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 H₂:CO ratio syngas at 1500 psig. The reactorcontents were transferred under syngas pressure to a phase separationvessel where separation began immediately and 32.80 grams of lower layermaterial was isolated. Upper layer reaction liquor was recycled back tothe reactor. Compositions of the upper and lower layer are given inTable 3. Catalyst partition data is shown in Table 4. The averagedreaction rate through this recycle gave 34 g/L/hr.

EXAMPLE 13 Phase Separation Process, Recycle 5

[0069] The recycled reaction liquor from example 12 was heated to 90° C.An addition of 14.74 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 H₂:CO ratio syngas at 1500 psig. The reactorcontents were transferred under syngas pressure to a phase separationvessel where phase separtion began immediately and 71.90 grams of lowerlayer material was isolated. Upper layer reaction liquor was recycledback to the reactor. Compositions of the upper and lower layer are givenin Table 3. Catalyst partition data is shown in Table 4. The averagedreaction rate through this recycle gave 30 g/L/hr.

[0070] The three most important results for the phase separation are: 1)achieve an acceptable high enough rate of production of PDO, 2) recyclemost of the catalyst (in the upper phase), and 3) recover concentratedproduct (PDO) in the lower phase.

[0071] The data on rate of production of PDO in the examples above showsthat an acceptable rate of reaction is achieved and that the catalyst isactive after 5 recycles (#1).

[0072] Table 4 shows that a high percentage of the catalyst is directlyrecycled in the upper phase (#2).

[0073] Table 3 shows high recovery of PDO in the lower phase (#3). TABLE3 Phase Split Primary Compositions Example Layer PDO % w MTBE % w Mass(g)  8 Lower 59.70 18.13 12.94  9 Lower 47.97 16.60 8.22 10 Lower 45.9719.15 8.50 11 Lower 47.32 21.73 19.50 12 Lower 45.16 20.99 32.80 13Lower 47.50 25.78 71.90  8 Upper 4.74 85.70 152.36  9 Upper 5.15 87.16160.04 10 Upper 17.67 77.60 167.19 11 Upper 27.31 54.86 163.47 12 Upper14.41 69.85 147.04 13 Upper 10.59 80.36 93.46

[0074] TABLE 4 Catalyst Species Partition Data Example Layer % ofAvailable Catalyst (Co; Ru)  8 Upper 90; 88  9 Upper 91; 88 10 Upper 93;91 11 Upper 82; 75 12 Upper 78; 71 13 Upper 61; 75  8 Lower 10; 12  9Lower  9; 12 10 Lower 7; 9 11 Lower 18; 25 12 Lower 21; 29 13 Lower 38;25

EXAMPLE 14 Phase Separation Catalyst Recycle/Product Process withCatalyst Prepared Via Stepwise Procedure

[0075] In an inert atmosphere drybox, to a 300 ml 2.14 grams (6.90mmole) 1,2-bis(9-phosphacyclononyl) ethane, 0.694 grams (3.25 mmole Ru)triruthenium dodecylcarbonyl, 119 grams methyl tert-butyl ether (MTBE)was added. The autoclave body was sealed and fitted to a benchscaleprocess unit. Under a headspace of 4:1 (H₂:CO) syngas at 1500 psig themixture was allowed to reach equilibrium over 1 hour at 105C. To thereactor a solution of, 1.11 grams (6.50 mmole Co) dicobalt octacarbonyland 0.108 grams (1.32 mmole) sodium acetate in 33.3 grams MTBE was addedat reaction conditions. The catalyst was allowed to preform at 105° C.and 1500 psig for 1.75 hours. Reactor temperature was reduced to 90° C.Two separate additions totaling 13.2 grams of ethylene oxide (EO) weremade and allowed to react with a 2:1 (H₂:CO, syngas feed untilsustantially all of the EO was consumed. The reactor contents weretransferred under syngas pressure to a temperature controlled phaseseparation vessel. The phase separation was allowed to equilibrate at43° C. A lower phase of 36.8 grams was isolated. Upper phase wasrecycled back to the reactor. Compositions of the upper and lower phaseare given in Table 5. Catalyst partition data is shown in Table 6. Theproduct, 1,3-propanediol was produced at an average rate of 26 g/L/hr.

EXAMPLE 15 Phase Separation Process, Recycle 1

[0076] The recycled reaction liquor from example 14 was heated to 90° C.An addition of 14.74 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 syngas at 1500 psig. The reactor content wastransferred under syngas pressure to a phase separation vessel. Whenequilibrated to 43° C., 28.5 grams of lower phase material was isolated.Upper phase reaction liquor was recycled back to the reactor.Compositions of the upper and lower phase are given in Table 5. Catalystpartition data is shown in Table 6. The averaged reaction rate throughthis recycle gave 24 g/L/hr.

EXAMPLE 16 Phase Separation Process, Recycle 2

[0077] The recycled reaction liquor from example 15 was heated to 90° C.An addition of 11.00 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 syngas at 1500 psig. The reactor content wastransferred under syngas pressure to a phase separation vessel. Whenequilibrated to 43° C., 24.8 grams of lower phase material was isolated.Upper phase reaction liquor was recycled back to the reactor.Compositions of the upper and lower phase are given in Table 5. Catalystpartition data is shown in Table 6. The averaged reaction rate throughthis recycle gave 35 g/L/hr.

EXAMPLE 17 Phase Separation Process, Recycle 3

[0078] The recycled reaction liquor from example 16 was heated to 90° C.An addition of 11.00 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 syngas at 1500 psig. The reactor contents weretransferred under syngas pressure to a phase separation vessel. Whenequilibrated to 43° C., 19.1 grams of lower phase material was isolated.Upper phase reaction liquor was recycled back to the reactor.Compositions of the upper and lower phase are given in Table 5. Catalystpartition data is shown in Table 6. The averaged reaction rate throughthis recycle gave 23 g/L/hr.

EXAMPLE 18 Phase Separation Process, Recycle 4

[0079] The recycled reaction liquor from example 17 was heated to 90° C.An addition of 11.00 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 syngas at 1500 psig. The reactor content wastransferred under syngas pressure to a phase separation vessel. Whenequilibrated to 43° C., 38.9 grams of lower phase material was isolated.Upper phase reaction liquor was recycled back to the reactor.Compositions of the upper and lower phase are given in Table 5. Catalystpartition data is shown in Table 6. The averaged reaction rate throughthis recycle gave 18 g/L/hr.

EXAMPLE 19 Phase Separation Process, Recycle 5

[0080] The recycled reaction liquor from example 18 was heated to 90° C.An addition of 11.00 grams ethylene oxide was made and allowed to reactunder a head space of 2:1 syngas at 1500 psig. The reactor content wastransferred under syngas pressure to a phase separation vessel. Whenequilibrated to 43° C., 38.9 grams of lower phase material was isolated.Upper phase reaction liquor was recycled back to the reactor.Compositions of the upper and lower phase are given in Table 5. Catalystpartition data is shown in Table 6. The averaged reaction rate throughthis recycle gave 17 g/L/hr.

[0081] The data on rate of production of PDO in the examples above showsthat an acceptable rate of reaction is achieved and that the catalyst isactive after 5 recycles (#1).

[0082] Table 6 shows that a high percentage of the catalyst is directlyrecycled in the upper phase (#2).

[0083] Table 5 shows high recovery of PDO in the lower phase (#3). TABLE5 Phase Split Primary Compositions Example Layer PDO % w MTBE % w Mass(g) 14 Lower 63.68 16.15 24.80 15 Lower 49.68 17.39 28.50 16 Lower 68.0818.03 24.80 17 Lower 53.34 24.31 19.10 18 Lower 33.32 19.39 38.90 19Lower 30.03 25.91 29.80 14 Upper  7.20 44.63 165.07  15 Upper  8.8961.35 152.73  16 Upper 36.69 48.66 139.09  17 Upper 16.88 54.86 131.42 18 Upper  6.14 86.65 104.92  19 Upper 27.30 34.57 88.12

[0084] TABLE 4 Catalyst Species Partition Data Example Layer % ofAvailable Catalyst (Co; Ru) 14 Upper 70; 67 15 Upper 82; 68 16 Upper 85;72 17 Upper 89; 73 18 Upper 67; 63 19 Upper 73; 73 14 Lower 30; 33 15Lower 18; 32 16 Lower 15; 28 17 Lower 11; 27 18 Lower 33; 37 19 Lower27; 27

EXAMPLE 20 Recycle of Lower Phase Stepwise Assembled Catalyst

[0085] Lower layer samples from examples 14 and 15 rich in1,3-propanediol product were distilled at 90-110° C. under vaccumconditions of 60-4 mm Hg. Collections of methyl tert-ether solvent and1,3-propanediol were made on the column overhead. Overhead material wasgreater than 92% 1-3, propanediol. The distillation was carried out suchthat 75% of the initial charge mass was distilled. A 10 gram sample ofthe distillation bottoms containing recycled catalyst, some1-3,propanediol and minor amounts of heavy ends was inventoried into a300 ml autoclave in an inert atmosphere drybox. To the autoclave wasadded 74 grams of fresh methyl tert-butyl ether solvent. The autoclavewas sealed and fitted to a benchscale process unit. The catalyst liquorwas heated to 90° C. with stirring. Under a headspace of 4:1 (H₂:CO)syngas, 11.00 grams of ethylene oxide was added and allowed to react.The reactor contents was transferred under syngas pressure to a phaseseparation vessel where at 45° C. phase separation began. Whenequilibrated, 12.6 grams of lower phase material was isolated. Thislower phase contained 56.47% 1,3-propanediol product. Upper phasereaction liquor was recycled back to the reactor and heated to 90° C.under a syngas feed headspace of 2:1 (H₂:CO). To this recycled solventphase, 11.00 grams of ethylene oxide was added and allowed to react. Thereactor contents were transferred under syngas pressure to a phaseseparation vessel where at 43° C. phase separation began. Whenequilibrated, 24.5 grams of lower phase material was isolated. Thislower phase contained 45.14% 1,3-propanediol product. These reactionsafforded an 81% product yield. This proves that the catalyst is robustand still active even after being distilled from the product phase andrecycled twice through the upper phase of subsequent reactions.

EXAMPLE 21 Use of Hexane as Phase Split Inducing Agent

[0086] In an inert atmosphere drybox, to a 300 ml autoclave, 1.159 grams(3.73 mmole) 1,2-bis(9-phosphacyclononyl) ethane, 0.696 grams (3.27mmole Ru) triruthenium dodecylcarbonyl, 119 grams methyl tert-butylether (MTBE) was added. The autoclave body was sealed and fitted to abenchscale process unit. Under a headspace of 4:1 (H₂:CO) syngas at 1500psig the mixture was allowed to reach equilibrium over 1.5 hour at 105°C. To the reactor a solution of, 1.13 grams (6.50 mmole Co) dicobaltoctacarbonyl and 0.108 grams (1.32 mmole) sodium acetate in 33.3 gramsMTBE was added at reaction conditions. The catalyst was allowed topreform at 105° C. and 1500 psig for 1.75 hours. Reactor temperature wasreduced to 90° C. One addition of 22 grams of ethylene oxide (EO) wasmade and allowed to react with a 2:1 (H₂:CO) syngas feed. The reactorcontents were transferred under syngas pressure to a temperaturecontrolled phase separation vessel. The phase separation was allowed toequilibrate at 43° C. A lower phase of 9.746 grams was isolated. Upperphase was recycled back to the reactor. As in a fashion similar to aboveexamples additional ethylene oxide was added to the recycled upper layerand allowed to react followed by a temperature induced phase split. Onthe third recycle in this example 11.00 grams of ethylene oxide wasadded and allowed to react at 90° C. and 1500 psig. Transfer to phaseseparation vessel and subsequent to cooling to 35° C., no phaseseparation was apparent. Two separate additions of 11.00 gram aliquotsof ethylene oxide followed by reaction at stated conditions, and coolingto 33° C. did not produce a 1,3-propanediol concentration where a phaseseparation could be made. We believe that this reaction produced someby-products, such as ethanol and propanol, that are miscibilizing innature that prevented the phase separation. Addition of 10 grams ofhexane while in the reactor at stated conditions followed by transfer tothe separation vessel and cooling invoked a phase separation at 77° C.This is one way to change the polarity of the system such that a phasesplit can be induced. It is even possible to add before or during thereaction miscibilizing agents to ensure a single phase reaction. Thesemiscibilizing agents can then be removed, such as by distillation orflashing, to invoke a phase split for product recovery. Afterequilibrating to 430° C., the a lower layer sample of 92.7 grams wasisolated and contained 48% 1,3-propanediol product.

We claim:
 1. A process for preparing a hydroformylation catalyst whichinvolves: a) forming a complex (A) by contacting a ruthenium (0)compound with a ditertiary phosphine ligand; and b) forming a complex(B) by subjecting complex (A) to a redox reaction with a cobalt(0)carbonyl compound.
 2. The process of claim 1, wherein the ditertiaryphosphine ligand is of the general formula: RRP—Q—PR′R′ wherein eachgroup R and R′ independently or jointly is a hydrocarbon moiety of up to30 carbon atoms, and Q is an organic bridging group of 2 to 4 atoms inlength.
 3. The process of claim 2, wherein group R or R′ eachindependently is an alkyl, cycloalkyl, bicycloalkyl or aryl group. 4.The process of claim 3, wherein group R or R′ each independently has upto 20 carbon atoms.
 5. The process of claim 2, wherein group Q iscomposed of carbon atoms.
 6. The process of claim 5, wherein Q is analkylene group of 2, 3 or 4 carbon atoms in length.
 7. The process ofclaim 2, wherein both groups R and/or R′ are part of a bivalent group,forming with the phosphorus atom a phosphacycloalkane of from 5 to 8atoms, which itself may be part of a multiring system.
 8. The process ofclaim 2, wherein the ditertiary phosphine ligand is selected from anyone or more of 1,2-bis(dicyclohexylphosphino)ethane,1,2-bis(diphenylphosphino)ethane, 1,2-bis(diethylphosphino)ethane,1-(diethylphosphino)-3-(dibutylphosphino)propane,1,2-bis(diphenylphosphino)benzene, 1,2-bis(dimethylphosphino)ethane,1,2-bis(2,4,4-trimethylpentylphosphino)ethane,1,2-bis(diisobutylphosphino)ethane, 1,2-P,P′-bis(9-phosphabicyclo[3.3.1]and/or [4.2.l]nonyl)ethane, its 1,2-P,P′-propane, or its1,3-P,P′-propane analogue.
 9. The process of claim 1, wherein the ratioof ligand to ruthenium atom varies from 2:1 to 1:2.
 10. The process ofclaim 9, wherein the ratio of ligand to ruthenium atom varies from 3:2to 2:3.
 11. The process of claim 9, wherein the ratio of ligand toruthenium atom is about 1:1.
 12. The process of claim 1, whereintriruthenium(0) dodecacarbonyl is used.
 13. The process of claim 1,wherein dicobalt octacarbonyl is used.
 14. The process of claim 1,wherein the molar ratio of ruthenium to cobalt varies from 4:1 to 1:4.15. The process of claim 14, wherein the molar ratio of ruthenium tocobalt varies from 2:1 to 1:3.
 16. The process of claim 14, wherein themolar ratio of ruthenium to cobalt varies from 1:1 to 1:2.
 17. Theprocess of claim 14, wherein the complex (B) is made by a step-wisemethod.
 18. The process of claim 17, wherein the ruthenium (0) compoundis reacted with the ditertiary phosphine ligand in the presence ofsyngas.
 19. The process of claim 17, wherein the ruthenium (0) compoundis reacted with the ditertiary phosphine ligand in the presence of asolvent.
 20. The process of claim 19, wherein the solvent comprises anether.
 21. The process of claim 19, wherein the solvent is methyltert.butyl ether.
 22. The process of claim 17, wherein the ruthenium (0)compound is reacted with the ditertiary phosphine ligand at atemperature within the range of 90 to 130 C.
 23. The process of claim17, wherein complex (A) is caused to undergo a redox reaction with acobalt(0) carbonyl compound at a temperature within the range of 90 to130° C.
 24. A hydroformylation catalyst prepared by a process whichinvolves: a) forming a complex (A) by contacting a ruthenium (0)compound with a ditertiary phosphine ligand; and b) forming a complex(B) by subjecting complex (A) to a redox reaction with a cobalt(0)carbonyl compound.
 25. The hydroformylation catalyst of claim 24,wherein the metal being ligated is ruthenium, rather than cobalt. 26.The hydroformylation catalyst of claim 24, characterized by having acobalt carbonyl anion IR band at 1894 cm⁻¹.
 27. A one stephydroformylation process for preparing a 1,3-diol, comprising thereaction of an oxirane with syngas at hydroformylation conditions in aninert solvent in the presence of a hydroformylation catalyst prepared bya process which involves: a) forming a complex (A) by contacting aruthenium (0) compound with a ditertiary phosphine ligand; and b)forming a complex (B) by subjecting complex (A) to a redox reaction witha cobalt(0) carbonyl compound.
 28. The process of claim 27, wherein theoxirane has up to 10 carbon atoms.
 29. The process of claim 27 whereinethylene oxide is used as oxirane.
 30. The process of claim 27, whereinthe molar ratio of hydrogen and carbon monoxide in the syngas variesfrom 1:1 to 8:1.
 31. The process of claim 27, wherein the reaction isconducted at a temperature ranging from ambient temperature to 150° C.32. The process of claim 27, wherein the reaction is conducted at areaction pressure in the range from 5 to 15 MPa.
 33. The process ofclaim 27, wherein the reaction is conducted in the presence of asolvent.
 34. The process of claim 33, wherein the solvent comprises anether.
 35. The process of claim 27, wherein the oxirane is maintainedthroughout the reaction in a concentration not less than about 0.2% byweight.
 36. The process of claim 35, wherein the oxirane is maintainedthroughout the reaction within the range of 0.2 to 20% by weight. 37.The process of claim 36, wherein the oxirane is maintained throughoutthe reaction within the range of 1 to 10% by weight.
 38. The process ofclaim 27, wherein at the conclusion of the hydroformylation reaction,the product mixture is recovered by selective extraction, fractionaldistillation, phase separation, decantation, and/or selectivecrystallization of a diol rich phase from the reaction mixture.
 39. Theprocess of claim 27, wherein at the conclusion of the hydroformylationreaction, the catalyst is recycled.
 40. The process of claim 2, whereinthe groups R and R′ of the tertiary phosphine ligand are each part of aring system with one of the two phosphorus atoms.
 41. The process ofclaim 40, wherein the ditertiary phosphine ligand is abis(phospholano)alkane.
 42. The process of claim 41, wherein thebis(phospholano)alkane is selected from the group consisting of1,2-bis(phospholano)ethane and 1,2-bis(2,5-dimethylphospholano)ethane.43. A one step hydroformylation process for preparing a 1,3-diol,comprising the reaction of an oxirane with syngas at hydroformylationconditions in an inert solvent in the presence of a hydroformylationcatalyst which is a ruthenium (+1)-phosphine bidentate:cobalt (−1)complex wherein the ligated metal is ruthenium, under conditions whichpreferably upon completion of the oxirane/syngas reaction cause a phaseseparation of the reaction mixture into an upper solvent phase which isrich in catalyst and a lower phase which is rich in the 1,3-diol,recycling the upper phase rich in catalyst directly to thehydroformylation reaction for further reaction with previously unreactedstarting materials, and recovering the 1,3-diol from the lower phaserich in 1,3-diol.
 44. The process of claim 43 wherein the catalyst isprepared by either (1) forming a complex (A) by contacting a ruthenium(0) compound with a ditertiary phosphine ligand and forming a complex(B) by subjecting complex (A) to a redox reaction with a cobalt(0)carbonyl compound or (2) bringing all the foregoing components togetherat the same time under conditions selected to favor the formation of aligated ruthenium species.
 45. The process of claim 43 wherein thetemperature during phase separation is from just above the freezingpoint of the reaction mixture to at least 150° C.
 46. The process ofclaim 45 wherein the temperature during phase separation is from 27 to97° C.
 47. The process of claim 46 wherein the temperature during phaseseparation is from 37 to 47° C.
 48. The process of claim 43 wherein theconcentration of the 1,3-diol is from 1 to 50% by weight.
 49. Theprocess of claim 48 wherein the concentration of the 1,3-diol is from 8to 32% by weight.
 50. The process of claim 49 wherein the concentrationof the 1,3-diol is from 16 to 20% by weight.
 51. The process of claim 43wherein the oxirane concentration is not less than 0.2% by weight. 52.The process of claim 51 wherein the oxirane concentration from 0.2 to20% by weight.
 53. The process of claim 52 wherein the oxiraneconcentration is from 1 to 10% by weight.
 54. The process of claim 43wherein the temperature during phase separation is from just above thefreezing point of the reaction mixture to at least 150° C., theconcentration of the 1,3-diol is from 1 to 50% by weight, and theoxirane concentration is not less than 0.2% by weight.
 55. The processof claim 54 wherein the temperature during phase separation is from 27to 97° C., the concentration of the 1,3-diol is from 8 to 32% by weight,and the oxirane concentration from 0.2 to 20% by weight.
 56. The processof claim 55 wherein the temperature during phase separation is from 37to 47° C., the concentration of the 1,3-diol is from 16 to 20% byweight, and the oxirane concentration is from 1 to 10% by weight.
 57. Ahydroformylation catalyst which is a ruthenium (+1)-phosphinebidentate:cobalt (−1) complex wherein the ligated metal is ruthenium.58. The hydroformylation catalyst of claim 57 wherein the catalyst isprepared by either (1) forming a complex (A) by contacting a ruthenium(0) compound with a ditertiary phosphine ligand and forming a complex(B) by subjecting complex (A) to a redox reaction with a cobalt(0)carbonyl compound or (2) bringing all the foregoing components togetherat the same time under conditions selected to favor the formation of aligated ruthenium species.